CN203845966U - Clear separating and refining device for catalytic cracking dry gas with high yield and high purity - Google Patents
Clear separating and refining device for catalytic cracking dry gas with high yield and high purity Download PDFInfo
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
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- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
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Abstract
The utility model relates to a clear separating and refining device for a catalytic cracking dry gas with high yield and high purity. The device comprises a first compressor, a second compressor, a first pressure swing adsorption tower, a second pressure swing adsorption tower, a membrane separating device and a cryogenic separation system, wherein the output end of the first compressor is connected with the inlet at the bottom of the first pressure swing adsorption tower and the top of the first pressure swing adsorption tower is connected with the inlet at the bottom of the second pressure swing adsorption tower; the outlets at the bottom of the first and the second pressure swing adsorption towers are connected with the input end of the second compressor; the output end of the second compressor is connected with the membrane separating device, the permeation side of the membrane separating device is further connected with the inlet at the bottom of the first pressure swing adsorption tower, and the non-permeation side of the membrane separating device is connected with the cryogenic separation tower system. By adopting a technology of combining pressure swing adsorption, membrane separation and cryogenic separation, the device provided by the utility model makes up the respective deficiencies of the three processes and can clearly separate and recover hydrogen, light alkane and light olefins in the refinery dry gas.
Description
Technical field
The utility model belongs to chemical field, relates to the highly purified catalytic cracked dry gas sharp separation of a kind of high yield refining plant.
Background technology
Useful component in oil refinery dry gas is mainly hydrogen, light olefin and light alkane etc.These components are all of great value in refinery, but they still do not realize optimum use very in a large number at present, but have directly been used as fuel, the even direct ignition torch emptying having.Catalytic cracked dry gas for the amount of accounting for maximum in oil refinery dry gas, had both contained hydrogen, also contained a large amount of light olefins and light alkane.These components can be separated respectively and utilize, higher than the raw material benefit that it is directly used as to fuel or reformation hydrogen production, synthesizing methanol.
At present, the research and development of the comprehensive utilization technique of plant catalytic cracking (FCC) dry gas mainly concentrate on three large fields: the one, and dry gas purification is refining, and the 2nd, the separation and purification of each component, the 3rd, the technology such as the chemical process utilization of each component.Wherein, the complete sharp separation of each component of FCC dry gas is refining is a kind of good method of dry gas comprehensive utilization economic benefit.
The technology that reclaims low-concentration hydrogen, light olefin and light alkane from FCC dry gas mainly contains separation by deep refrigeration, middle cold-peace shallow cold oil absorption process, membrane separation process, adsorption method of separation etc.
Adsorption method of separation is to utilize sorbent material different to the adsorption selectivity of each component in mixed gas, by pressure or temperature change, realize a kind of separation method of absorption and regeneration, there is the features such as reproduction speed is fast, energy consumption is low, simple to operate, technical maturity is stable.By pressure change, realizing separated pressure-variable adsorption, to reclaim in dry gas hydrogen technique relatively ripe, and can obtain purity is 98%(volume ratio) above hydrogen product, but hydrogen recovery rate is generally in 80-85% left and right.Adopt the existing PSA Technology will be from containing reclaim highly purified hydrogen, ethene and ethane the FCC dry gas such as low-concentration hydrogen, ethene simultaneously, exist yield low, can not realize the complete sharp separation of FCC dry gas main ingredient, the problems such as huge are taken up an area in investment.Such as, in the petrochemical industry FCC of China Petrochemical Industry dry gas recovering ethylene by pressure swing adsorption and hydrogen demonstration unit, the yield of ethene, hydrogen is lower than 75-80%, and cannot reclaim highly purified ethane propylene etc. simultaneously.
Membrane separation process is under certain pressure, utilizes the difference of other each components infiltration rate in film to carry out separated.Membrane separation process reclaims the 1987 Nian U.S. huge card city Okia that is installed on of hydrogen in FCC dry gas and builds up, and hydrogen recovery rate is 80-90%.Hydrogen recovery in the dry gas that membrane separation process is applicable to is with pressure, hydrogen content is low, that its advantage is to take up an area is little, simple to operate, energy consumption is low etc.But the hydrogen purity reclaiming by membrane separation process is not high, is generally 95-99%.And aspect recovery ethene, ethane, membrane separation technique is still in the development phase.
Cold separation technology just had and has developed as far back as the fifties in last century, at present this technology comparative maturity.It is the difference (boiling-point difference) of utilizing each component relative volatility in raw material, by gas turbine swell refrigeration, at low temperatures each component in dry gas is got off by processing requirement condensation, the hydrogen that is difficult for condensation obtains at first, hydrogen recovery rate is 92-95%, and purity is 95-98%.Thereafter with rectification method, wherein each class hydrocarbon is separated one by one, yield of ethene generally surpasses 85-90%.Low temperature separation process has simultaneously relatively advantages of higher of recover hydrogen and ethylene-ethane, technical maturity, the rate of recovery, and the general occasion that is applicable to processing a large amount of dry gas, is particularly suitable for area of concentration, refinery.The oil refinery dry gas recovery that low temperature separation process shortcoming is that product purity is not high, investment is large, energy consumption is high, be not suitable for middle and small scale etc.
The limitation of dry gas is reclaimed separately in, membrane sepn separated for pressure-variable adsorption and low temperature separation process separately, in technology at present, not too under mature condition, adopts process integration to contribute to improve separating effect and economy.
CN1085821A has proposed a kind of membrane sepn technique that combines with low temperature separation process, to catalytic cracked dry gas carry out hydrogen hydrocarbon separated with reclaim.The hydrogen purity that this process integration obtains is more than 95%, and hydrogen yield is more than 85%; The ethene obtaining has higher purity, and yield approaches 98%.Still there is the shortcomings such as product purity is low, hydrogen yield is low, energy consumption is high in this process integration.
CN101773765A has proposed a kind of membrane sepn combine technique separated with pressure-variable adsorption, and the hydrogen in catalytic cracked dry gas is carried out to Separation and Recovery.The hydrogen purity that this process integration obtains is 95-99.5%, hydrogen yield 80%.But this process integration does not relate to the recovery of ethene, ethane etc.
In sum, existing from plant catalytic cracking dry gas the process integration of the component such as recover hydrogen, ethylene-ethane, propylene simultaneously,, membrane sepn separated to pressure-variable adsorption, and the low temperature separation process not larger improvement of limitation of use separately, still there is the problems such as product purity is not high, yield is lower, can not realize that the complete sharp separation of each component of dry gas is refined.
Utility model content
In order to overcome, existing pressure-variable adsorption is separated, membrane sepn, and low temperature separation process exists that product purity is not high, yield is lower, can not realize the refining technological deficiency of the complete sharp separation of each component of dry gas while using separately, the utility model discloses a kind of highly purified catalytic cracked dry gas sharp separation of high yield refining plant.
The highly purified catalytic cracked dry gas sharp separation of high yield described in the utility model refining plant, comprises the first compressor, the second compressor, the first pressure-swing absorber, the second pressure-swing absorber, membrane separation unit and low temperature separation process system; It is characterized in that,
Described the first compressor output end is connected with import at the bottom of the first pressure-swing absorber tower, and described the first pressure-variable adsorption column overhead connects import at the bottom of the second pressure-swing absorber tower; The tower bottom outlet of described the first pressure-swing absorber and the second pressure-swing absorber is all connected with the second compressor input terminus;
Described the second compressor output end junctional membrane tripping device, the per-meate side of described membrane separation unit be also connected with import at the bottom of the tower of the first pressure-swing absorber, the non-per-meate side of described membrane separation unit is connected with described low temperature separation process system.
Preferably, between described the first air compressor and the first pressure-swing absorber, be also connected with depickling gas tower.
Preferably, between described the first air compressor and the first pressure-swing absorber, be also connected with dry gas refining plant.
Preferably, between described membrane separation unit and the second compressor, be also connected with except spray dust oil device.
Preferably, described low temperature separation process system comprises demethanizing tower and cold recovery system, and described demethanizing tower entrance is connected with the infiltrating gas side of described membrane separation unit, and demethanizer column overhead outlet is connected with cold recovery system.
Further, described low temperature separation process system also comprises ethene topping still, ethylene rectification tower, propylene topping still, propylene rectification tower; The import of described ethene topping still is connected with the tower bottom outlet of demethanizing tower, and described ethene topping still tower top outlet is connected with the entrance of ethylene rectification tower; Import is connected described ethene topping still tower bottom outlet with propylene topping still; Described ethylene rectification tower tower top flows out ethylene product, and tower bottom outlet turns back to ethene topping still; Described propylene topping still tower top flows out ethane product, and import is connected tower bottom outlet with propylene rectification tower.
Adopt the highly purified catalytic cracked dry gas sharp separation of high yield described in the utility model refining plant, adopt the technology of pressure-variable adsorption, membrane sepn, low temperature separation process triplicity, three kinds of defects that technique exists have separately been made up, for the hydrogen in oil refinery dry gas, light alkane and each component of light olefin have realized sharp separation recovery, have greatly improved yield and the purity of each gaseous fraction of oil refinery dry gas.
Accompanying drawing explanation
Fig. 1 illustrates a kind of embodiment structural representation of the highly purified catalytic cracked dry gas sharp separation of high yield described in the utility model refining plant;
Fig. 2 illustrates the embodiment schematic flow sheet based on Fig. 1;
In each figure, Reference numeral name is called: 1-first pressure-swing absorber 2-second pressure-swing absorber 3-first compressor 4-the second compressor 5-membrane separation unit 6-depickling gas tower 7-demethanizing tower 8-ethene topping still 9-propylene topping still 10-cold recovery system 11-ethylene rectification tower 12-propylene rectification tower 13-is except spray dust oil device 14-dry gas refining plant.
Embodiment
Below in conjunction with accompanying drawing, embodiment of the present utility model is described in further detail.
The utility model discloses the highly purified catalytic cracked dry gas sharp separation of a kind of high yield refining plant, to realize aforesaid method.Comprise the first compressor, the second compressor, the first pressure-swing absorber, the second pressure-swing absorber, membrane separation unit and low temperature separation process system; Described the first compressor output end is connected with import at the bottom of the first pressure-swing absorber tower, and described the first pressure-variable adsorption column overhead connects import at the bottom of the second pressure-swing absorber tower; The tower bottom outlet of described the first pressure-swing absorber and the second pressure-swing absorber is all connected with the second compressor input terminus; Described the second compressor output end junctional membrane tripping device, the per-meate side of described membrane separation unit be also connected with import at the bottom of the tower of the first pressure-swing absorber, the non-per-meate side of described membrane separation unit is connected with described low temperature separation process system.
FCC dry gas in refinery, after the first compressor 3 pressurization, carries out pressure-variable adsorption at the bottom of entering the first pressure-swing absorber 1 tower, discharges ethylene-rich dry gas at the bottom of tower.The hydrogen not being adsorbed, methane and nitrogen etc. flow out from the first pressure-variable adsorption tower top, from the second pressure-swing absorber 2 bottoms, enter, the methane being adsorbed, nitrogen and a small amount of hydrogen, by reverse step-down process, from sorbent material, desorb, at the bottom of the second pressure-swing absorber, discharge, form the second stripping gas.Wherein, the second stripping gas can part emptying.The hydrogen that is not adsorbed agent absorption flows out from the second pressure-variable adsorption tower top, obtains hydrogen product.
After mixing, the second stripping gas and ethylene-rich dry gas mixed by the second compressor 4 pressurizations, the ethylene-rich mixing dry gas forming is sent into membrane separation unit 5 and is separated into infiltration gas and impermeable gas, infiltration gas main component is hydrogen, turn back to the first pressure-swing absorber 1, as the partial raw gas of the first pressure-swing absorber; Impermeable gas main component is olefines, methane and nitrogen, sends into the burning gas that low temperature separation process system adopts ordinary method separation to obtain ethane, ethene, propylene and is rich in methane.
Useful component in oil refinery dry gas is mainly hydrogen, light olefin and light alkane etc., but also has a small amount of oxygen, carbonic acid gas, sulfurous gas, oxynitride, mercaptan, carbonylsulfide and mercury, arsenic etc.Preferably, in step 101, rapid to increasing the depickling jia bombardier of oil refinery dry gas after oil refinery dry gas pressurization, adopt traditional amine to wash soda-wash tower, remove sour gas wherein.Another kind of advantageous measure is after oil refinery dry gas pressurization or after depickling gas, increases dry gas purification step, and so-called dry gas purification step, adopts conventional hydrogenation deoxidation reactor to carry out deoxidation, hydrogenation reduction device denitrogenation oxygen compound (N
xo
y), mercaptan removal (RSH) and carbonylsulfide (COS), and demercuration/arsenic device of conventional loading gac and molecular sieve forms.These two kinds of advantageous measure have further purified oil refinery dry gas, avoid the poison deactivation such as sorbent material, membrane module situation in subsequent step to occur, and improve segregation rate and product yield.
Membrane separation technique separating hydrogen gas is existing mature technology, and in step 104 of the present invention, membrane separation unit can use polycarbonate membrane to carry out separation to hydrogen, better to Hydrogen Separation effect.
In step 104, can enter before membrane separation unit at ethylene-rich mixing dry gas, the preferred demist dedusting deoiling step that increases, by the impurity removals such as micro-water smoke, dust and oil droplet in the ethylene-rich mixing dry gas of the 1.0-3.5MPa pressure obtaining in step 103, avoid membrane module in contaminate subsequent membrane sepn step, membrane component and prolong work-ing life.Except spray dust oil, can adopt the equipment such as conventional loading gac mist eliminator, 50-200 order wire cloth oil droplet, dust catching device to realize.
Preferably, described low temperature separation process system comprises demethanizing tower and cold recovery system, and described demethanizing tower entrance is connected with the infiltrating gas side of described membrane separation unit, and demethanizer column overhead outlet is connected with cold recovery system.With the separation realizing in abovementioned steps 105, be rich in the burning gas of methane the step of refrigeration.The methane that demethanizing tower top is discharged and nitrogen input cold recovery system swell refrigeration, output cold, discharges burning gas simultaneously from cold recovery system.Cold recovery system can be comprised of conventional decompressor and ice chest.
Adopt aforesaid method separation of methane, utilize methane and the nitrogen expansion refrigeration that demethanizer column overhead is discharged to obtain cold, during for components such as later separation ethene, ethane, propylene.
Further, described low temperature separation process system also comprises ethene topping still, ethylene rectification tower, propylene topping still, propylene rectification tower; To realize the separated of follow-up ethene, ethane and propylene.The import of wherein said ethene topping still is connected with the tower bottom outlet of demethanizing tower, and described ethene topping still tower top outlet is connected with the entrance of ethylene rectification tower; Import is connected described ethene topping still tower bottom outlet with propylene topping still; Described ethylene rectification tower tower top flows out ethylene product, and tower bottom outlet turns back to ethene topping still; Described propylene topping still tower top flows out ethane product, and import is connected tower bottom outlet with propylene rectification tower; Described propylene rectification tower tower top flows out propylene, and tower bottom flow goes out C
3above cut.
The carbon two component pneumatic transmissions of discharging at the bottom of demethanizer enter ethene topping still, and ethene topping still tower top outflow material enters the rectifying of ethylene distillation column overhead and goes out ethene, and ethylene rectification tower bottom stream matter turns back to ethene topping still; Ethene topping still bottom stream matter is sent into propylene topping still, and propylene topping still tower top flows out ethane, bottom stream matter send into the rectifying of propylene rectification tower tower top and go out propylene, tower at the bottom of rectifying go out C
3above cut.The required cold of ethene, propylene, ethane fractionation is from the cold obtaining in above-mentioned swell refrigeration process.
As Fig. 1 illustrates a kind of embodiment of the highly purified catalytic cracked dry gas sharp separation of high yield described in the utility model refining plant, adopt the method flow shown in corresponding diagram 2.
FCC dry gas in refinery is removed after foreign gases through the first compressor 3 pressurizations, depickling gas tower 6 depickling gas, dry gas refining plant 14, carries out pressure-variable adsorption at the bottom of entering the first pressure-swing absorber 1 tower, discharges ethylene-rich dry gas at the bottom of tower.The hydrogen not being adsorbed, methane and nitrogen etc. flow out from the first pressure-variable adsorption tower top, from the second pressure-swing absorber 2 bottoms, enter, the methane being adsorbed, nitrogen and a small amount of hydrogen, by reverse step-down process, from sorbent material, desorb, at the bottom of the second pressure-swing absorber, discharge, form the second stripping gas.Wherein, the second stripping gas can part emptying.The hydrogen that is not adsorbed agent absorption flows out from the second pressure-variable adsorption tower top, obtains hydrogen product.
After mixing, the second stripping gas and ethylene-rich dry gas mixed by the second compressor 4 pressurizations, the ethylene-rich mixing dry gas forming is sent into membrane separation unit 5 and is separated into infiltration gas and impermeable gas through remove steam dust wherein and oil droplet except spray dust oil device 13 after, infiltration gas main component is hydrogen, turn back to the first pressure-swing absorber 1, as the partial raw gas of the first pressure-swing absorber; Impermeable gas main component is olefines, methane and nitrogen, send into demethanizing tower 7, demethanizer column overhead is discharged methane and nitrogen, enter cold recovery system 10 swell refrigerations, demethanizing tower tower bottom flow goes out composition and enters ethene topping still 8, ethene topping still tower top and flow out material and enter ethylene rectification tower 11 rectifying and go out ethene, and ethylene distillation tower bottom flow goes out composition and turns back to ethene topping still; Ethene topping still bottom stream matter is sent into propylene topping still 9, and propylene topping still tower top flows out material ethane, and propylene topping still bottom stream matter is sent into propylene rectification tower 12 tower top rectifying and gone out propylene, and at the bottom of tower, rectifying goes out C
3above cut.The required cold of ethene, propylene, ethane fractionation is from the cold obtaining in above-mentioned swell refrigeration process.
Adopt method flow and the device shown in Fig. 1 to 2, each component recovery and the purity that under the different oil refinery dry gas of process element and different reaction conditions, obtain are as follows:
Hydrogen content 57.9%, methane content 22.2%, ethane content 7.5%, ethylene content 4.5%, propylene content 1.5%, a nitrogen content 5.5%, CO in embodiment 1. unstripped gass
2content 0.1%, sulphur content 50ppm, oxygen content 0.65%, other components 0.15%, wherein content is volume ratio (V/V).
The first compressor pressurizes is to 0.7MPa, the first pressure-swing absorber service temperature is that 30 degrees Celsius, the second pressure-swing absorber service temperature are that 30 degrees Celsius, the second compressor pressurizes to 2.0MPa, membrane sepn service temperature are 35 degrees Celsius, when the cryogenic temperature that cold recovery system provides is-120 degrees Celsius
Hydrogen recovery rate and purity are respectively 90% and 99.9%, and methane recovery and purity are respectively 85% and 92%, and Recovery rate of ethylene and purity are respectively 92% and 99%, and the propylene rate of recovery and purity are respectively 92% and 99%, and ethane recovery and purity are respectively 90% and 99%.
Hydrogen content 46.5%, methane content 20.0%, ethane content 12.4%, ethylene content 6.0%, propylene content 0.6%, a nitrogen content 9.5%, CO in embodiment 2. unstripped gass
2content 0.1%, CO content 0.5%, butane 2.0%, pentane 1.0%, other components 0.15%, wherein content is volume ratio (V/V).
The first compressor pressurizes is to 1.2MPa, the first pressure-swing absorber service temperature is that 40 degrees Celsius, the second pressure-swing absorber service temperature are that 40 degrees Celsius, the second compressor pressurizes to 2.6MPa, membrane sepn service temperature are 50 degrees Celsius, when the cryogenic temperature that cold recovery system provides is-100 degrees Celsius
Hydrogen recovery rate and purity are respectively 93% and 99.9%, and methane recovery and purity are respectively 89% and 92%, and Recovery rate of ethylene and purity are respectively 94% and 99%, and the propylene rate of recovery and purity are respectively 94% and 99%, and ethane recovery and purity are respectively 94% and 99%.
Hydrogen content 18.5%, methane content 30.0%, ethane content 14.5%, ethylene content 16.0%, propylene content 1.7%, a nitrogen content 14.5%, CO in embodiment 3. unstripped gass
2content 1.7%, water-content 0.02%, other components (3.08%), wherein content is volume ratio (V/V).
The first compressor pressurizes is to 1.0MPa, the first pressure-swing absorber service temperature is that 35 degrees Celsius, the second pressure-swing absorber service temperature are that 35 degrees Celsius, the second compressor pressurizes to 3.2MPa, membrane sepn service temperature are 40 degrees Celsius, when the temperature of reaction that cold recovery system provides is-105 degrees Celsius
Hydrogen recovery rate and purity are respectively 92% and 99.9%, methane recovery and purity are respectively 90% and 92%, Recovery rate of ethylene and purity are respectively 96% and 99.9%, and the propylene rate of recovery and purity are respectively 96% and 99%, and ethane recovery and purity are respectively 95% and 99%.
The above-mentioned rate of recovery and purity are all measured with volume ratio.
Adopt high yield highly purified catalytic cracked dry gas sharp separation process for purification of the present invention and device, adopt the technology of pressure-variable adsorption, membrane sepn, low temperature separation process triplicity, three kinds of defects that technique exists have separately been made up, for the hydrogen in oil refinery dry gas, light alkane and each component of light olefin have realized sharp separation recovery, yield and the purity of each gaseous fraction of oil refinery dry gas have greatly been improved, wherein the recovery purity of hydrogen, ethene, ethane, propylene all can reach 99%, is rich in methane concentration in the fuel gas of methane and also can reaches 92%.
Further, increased depickling jia bombardier suddenly and corresponding intrument, protected the normal running of subsequent step and installed work-ing life.
Further, first separating and reclaiming hydrogen in membrane sepn process, make the enrichment carbon two of non-per-meate side and the demethanizing tower that the above component mixed gas of carbon two enters cryogenic system, can reduce the treatment capacity of low temperature separation process, greatly reduce demethanizing tower refrigeration load, improve demethanizer column overhead dew point, make low temperature separation process processing ease, greatly reduce low temperature separation process facility investment and running cost.
Further, in demethanizing process, adopt gas expansion refrigeration to obtain cold for later separation, realized cold self-produced, saved equipment and cost.
In sum, advantage of the present invention and beneficial effect are:
1. the present invention processes oil refinery dry gas in conjunction with adsorption method of separation, membrane separation process and separation by deep refrigeration, can access highly purified hydrogen, ethene, ethane, propylene etc., guaranteed high yield, realized the sharp separation of hydrogen, ethene, ethane, propylene simultaneously, pressure-variable adsorption separation, membrane sepn have been overcome, and the independent limitation of using of low temperature separation process, and membrane sepn is combined with low temperature separation process, membrane sepn still exists the problems such as product purity is not high, yield is lower, can not realize that the complete sharp separation of each component of dry gas is refined while being combined with pressure-variable adsorption;
2. the present invention includes purifying step, can remove the sour gas in dry gas, can improve the work-ing life of two sections of pressure-variable adsorption-regeneration system rapidlys and film separating system, reduce running cost, and improve hydrogen purity;
3. the present invention includes drying step and demist dedusting deoiling step, can remove micro-water smoke, dust and oil droplet in gas, in the work-ing life of further improving film separating system, reduce membrane sepn running cost;
4. the present invention includes membrane sepn step, enrichment C2 cut, methane and a small amount of hydrogen that can obtain the regeneration of two sections of pressure-variable adsorptions-regeneration step carry out separation, hydrogen permeate is gone over, and turns back to two sections of pressure-variable adsorption-regeneration step, makes the final rate of recovery of hydrogen can reach more than 90%;
5. the present invention includes two sections of pressure-variable adsorption-regeneration step and membrane sepn step, hydrogen is first reclaimed, the first, can make low temperature separation process system throughput greatly reduce, demethanizing tower refrigeration load is reduced greatly; The second, the C such as the ethene in dehydrogenation gas, ethane
2above cut content increases, and the demethanizing tower top dew point in low temperature separation process system increases, and low temperature separation process operation is more prone to, C
2and C
2above cut separation efficiency increases, and the purity of the ethene that makes to reclaim, ethane, propylene all can be greater than 99%, yield is greater than 90-92%; The 3rd, little by the dehydrogenation gas pressure drop of the non-per-meate side of membrane sepn, suitably decompression, makes low temperature separation process system efficiency higher; The 4th, can reduce investment and the running cost of low temperature separation process equipment simultaneously;
6. the present invention includes cold recovery step, the cold obtaining, for low temperature separation process step, has been accomplished like this to the recycle of resource, thereby reduced energy consumption, reduced the input of cost.
Previously described is each preferred embodiment of the present invention, preferred implementation in each preferred embodiment is if not obviously contradictory or take a certain preferred implementation as prerequisite, each preferred implementation arbitrarily stack combinations is used, design parameter in described embodiment and embodiment is only the invention proof procedure for clear statement contriver, not in order to limit scope of patent protection of the present invention, scope of patent protection of the present invention is still as the criterion with its claims, the equivalent structure that every utilization specification sheets of the present invention and accompanying drawing content are done changes, in like manner all should be included in protection scope of the present invention.
Claims (6)
1. the highly purified catalytic cracked dry gas sharp separation of high yield refining plant, comprises the first compressor (3), the second compressor (4), the first pressure-swing absorber (1), the second pressure-swing absorber (2), membrane separation unit (5) and low temperature separation process system; It is characterized in that,
Described the first compressor output end is connected with import at the bottom of the first pressure-swing absorber tower, and described the first pressure-variable adsorption column overhead connects import at the bottom of the second pressure-swing absorber tower; The tower bottom outlet of described the first pressure-swing absorber and the second pressure-swing absorber is all connected with the second compressor input terminus;
Described the second compressor output end junctional membrane tripping device feeding side, the per-meate side of described membrane separation unit be also connected with import at the bottom of the tower of the first pressure-swing absorber, the non-per-meate side of described membrane separation unit is connected with described low temperature separation process system.
2. the highly purified catalytic cracked dry gas sharp separation of high yield refining plant as claimed in claim 1, is characterized in that, is also connected with depickling gas tower (6) between described the first compressor and the first pressure-swing absorber.
3. the highly purified catalytic cracked dry gas sharp separation of high yield refining plant as claimed in claim 1, is characterized in that, is also connected with dry gas refining plant (14) between described the first compressor and the first pressure-swing absorber.
4. the highly purified catalytic cracked dry gas sharp separation of high yield refining plant as claimed in claim 1, is characterized in that, is also connected with demist, dedusting oil device (13) between described membrane separation unit and the second compressor.
5. the highly purified catalytic cracked dry gas sharp separation of high yield refining plant as claimed in claim 1, it is characterized in that, described low temperature separation process system comprises demethanizing tower (7) and cold recovery system (11), described demethanizing tower entrance is connected with the impermeable gas side of described membrane separation unit (5), and demethanizer column overhead outlet is connected with cold recovery system.
6. the highly purified catalytic cracked dry gas sharp separation of high yield refining plant as claimed in claim 5, it is characterized in that, described low temperature separation process system also comprises ethene topping still (8), ethylene rectification tower (11), propylene topping still (9), propylene rectification tower (12);
The import of described ethene topping still (8) is connected with the tower bottom outlet of demethanizing tower, and the tower top outlet of described ethene topping still (8) is connected with the entrance of ethylene rectification tower (11); Import is connected described ethene topping still (8) tower bottom outlet with propylene topping still (9); Described ethylene rectification tower (11) tower top flows out ethylene product, and tower bottom outlet turns back to ethene topping still (8); Described propylene topping still (9) tower top flows out ethane product, and import is connected tower bottom outlet with propylene rectification tower (12).
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104030875A (en) * | 2014-05-23 | 2014-09-10 | 四川天采科技有限责任公司 | Method and device for clearly separating and refining high-yield high-purity catalytic cracking dry gas |
| CN107285986A (en) * | 2016-04-01 | 2017-10-24 | 四川天采科技有限责任公司 | A kind of method of full temperature journey pressure-variable adsorption separating ethene cracking gas |
| CN108011119A (en) * | 2017-12-18 | 2018-05-08 | 陕西省石油化工研究设计院 | The method and system of hydrogeneous exhaust gas coupling fuel cells clean electric power generation recycling |
| US10227272B2 (en) | 2015-06-15 | 2019-03-12 | Uop Llc | Processes and apparatuses for recovery of ethylene from hydrocarbons |
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2014
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104030875A (en) * | 2014-05-23 | 2014-09-10 | 四川天采科技有限责任公司 | Method and device for clearly separating and refining high-yield high-purity catalytic cracking dry gas |
| CN104030875B (en) * | 2014-05-23 | 2016-10-05 | 四川天采科技有限责任公司 | High yield highly purified catalytic cracked dry gas sharp separation process for purification and device |
| US10227272B2 (en) | 2015-06-15 | 2019-03-12 | Uop Llc | Processes and apparatuses for recovery of ethylene from hydrocarbons |
| CN107285986A (en) * | 2016-04-01 | 2017-10-24 | 四川天采科技有限责任公司 | A kind of method of full temperature journey pressure-variable adsorption separating ethene cracking gas |
| CN107285986B (en) * | 2016-04-01 | 2020-09-01 | 四川天采科技有限责任公司 | Method for separating ethylene pyrolysis gas by full-temperature-range pressure swing adsorption |
| CN108011119A (en) * | 2017-12-18 | 2018-05-08 | 陕西省石油化工研究设计院 | The method and system of hydrogeneous exhaust gas coupling fuel cells clean electric power generation recycling |
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